JP2005281131A - System and method for co-production of hydrogen and electrical energy - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a system and a method for co-production of hydrogen and electrical energy. <P>SOLUTION: The system for co-production of the hydrogen and the electrical energy includes a reformer (4) configured to generate a hydrogen-rich reformed oil (44) by receiving a reformer fuel and steam. The system further includes a separation unit (12) fluid-communicated with the reformer (4). The separation unit (12) is configured to separate the hydrogen from the reformed oil (44) by receiving the reformed oil (44) and to generate an exhaust gas (18). Also, the system includes a combuster (6) configured to generate thermal energy and a high-temperature compressed gas (22) by receiving the fuel for combustion. The combuster (6) is coupled with the reformer (4). A gas turbine generates the electrical energy and an expansion gas (30) by expanding the high-temperature compressed gas (22) and at least a portion of the thermal energy from the combuster (6) is used for generating the reformed oil (44) within the reformer (4). <P>COPYRIGHT: (C)2006,JPO&NCIPI

Description

  The present invention relates to energy generation systems, and more specifically to simultaneous production of hydrogen and electrical energy.

In recent years, various attempts have been made to use a combined cycle power generation system in which fuel is combusted in a combustor to generate a hot gas, and the hot gas drives a gas turbine to generate electric power. Combustors of combined cycle power systems are typically cooled by compressed air that is readily available in the plant. The use of compressed air to cool the combustor limits the lower limit of the combustor flame temperature, which can result in high nitrogen oxide (NO _x ) production and emissions.

  Co-production means generally produce a quantity of liquid fuel or chemical from the same feedstock as well as electricity. Co-production is based on the concept of producing chemicals or liquid fuels during lean power demand periods and using them to increase power production during peak periods. One of the most widely used fuels, the hydrogen produced in such co-production plants can be used in several ways, including power generation.

Typical steam reforming of hydrocarbon fuels such as natural gas is the primary means of hydrogen production. This reforming reaction is an endothermic reaction that requires external heat supply. This external heat is usually supplied by burning a portion of the fuel used for reforming or any fuel rich gas available in the reforming plant. This process is energy intensive and can produce significant amounts of nitrogen oxides (NO _x ).
US Patent Publication No. 2003/068260

With the advent of the hydrogen economy, demand for simultaneous production systems capable of generating hydrogen and electricity is expected to increase. Thus, while generating hydrogen and electrical energy in an efficient manner, there is a need to design the simultaneous production system capable of limiting the emissions of NO _x.

  In one aspect, a system for simultaneous production of hydrogen and electrical energy includes a reformer configured to receive reformer fuel and steam to produce hydrogen-rich reformate. The system further includes a separation unit in fluid communication with the reformer, the separation unit configured to receive the reformate and separate hydrogen from the reformate to produce exhaust gas. The system also includes a combustor configured to receive fuel for combustion and generate thermal energy and hot compressed gas, the combustor coupled to the reformer. Gas turbines expand hot compressed gas to produce electrical energy and expanded gas, and at least a portion of the thermal energy from the combustor is used to produce reformate in the reformer.

  In yet another aspect, a system for simultaneous production of hydrogen and electrical energy includes a reformer configured to receive reformer fuel and steam to produce hydrogen rich reformate. The system further includes a combustor configured to receive fuel for combustion and generate thermal energy and hot compressed gas, the combustor coupled to the reformer. The separation unit is in fluid communication with the reformer, and the separation unit is configured to receive the reformate and separate hydrogen from the reformate to produce exhaust gas. At least a portion of the thermal energy from the combustor is used to produce the reformate in the reformer. Gas turbines expand hot compressed gas to produce electrical energy and expanded gas. At least a portion of the thermal energy from the combustor is used to produce reformate in the reformer. The separation unit is configured to separate carbon dioxide from the reformed oil and recirculate at least a portion of the exhaust gas to the reformer.

  In yet another aspect, a method for simultaneous production of hydrogen and electrical energy includes reforming a reformer fuel and steam mixture in a reformer to produce a hydrogen rich reformate. . The method further includes the step of separating hydrogen from the reformed oil to produce exhaust gas. The method also includes burning fuel in a combustor to produce thermal energy and hot compressed gas, the combustor being coupled to a reformer. The hot compressed gas is expanded in a gas turbine to produce electrical energy and expanded gas, and at least a portion of the thermal energy from the combustor is used to produce reformate in the reformer. .

  In yet another aspect, a combustor reformer system includes a combustor configured to receive and burn fuel and oxidant to produce hot compressed gas and thermal energy. The reformer is in intimate contact with the combustor, and the reformer is configured to receive the reformer fuel and steam to produce hydrogen rich reformate. The reformer is coupled to the combustor and at least a portion of the thermal energy from the combustor is used to produce reformate within the reformer.

  These and other features, aspects and advantages of the present invention will be better understood by reading the following detailed description with reference to the accompanying drawings, in which like numerals represent like elements throughout the drawings.

  FIG. 1 schematically illustrates an example simultaneous production system 2 for generating hydrogen and electrical energy, including a turbine section 3 and a hydrogen generation section 5. This hydrogen generator includes a reformer 4 and a separation unit 12. The turbine section includes a combustor 6, a compressor 24, a gas turbine 26, and a rotor 46, and the turbine 26 drives the compressor 24 by the rotor. The reformer 4 is coupled to the combustor 6, and combustion heat from the combustor 6 is used in the reforming process of the reformer 4. As will be described in some detail below, the basic components of the co-production system 2 are mostly known, but the improvement in efficiency associated with known systems is a system with a recirculation flow path that increases system performance and efficiency. Obtained through strategic interconnection of components. The efficiency of a simultaneous production system is enhanced by energy recovery from its exhaust stream. In various embodiments of the simultaneous production system described herein, the oxidant used in the combustion process is ambient air. It is understood that any other oxidant stream containing the amount of oxygen required for combustion can be used for the same purpose.

During operation, the reformer 4 is configured to receive the fuel stream 8 and the steam 40. In the reformer 4, the fuel stream 8 reacts with the steam 40 to produce a hydrogen rich reformate stream 44. The reformed oil stream 44 is sent to the separation unit 12, which is configured to produce a substantially pure hydrogen stream 16 and an exhaust gas stream 18. In some embodiments, the separation unit 12 further produces a carbon dioxide (CO ₂ ) rich stream 14.

Typically, reforming hydrocarbon fuels such as natural gas with steam produces hydrogen. This process is energy intensive and a large amount of heat is absorbed throughout the reforming process. The main component of natural gas is methane (CH ₄ ), which reacts with steam in a two-stage reaction to produce hydrogen. During the reforming process, natural gas is converted to hydrogen according to reactions (1) and (2) shown below.
CH ₄ + H ₂ O => CO + 3H ₂ (1)
CO + H ₂ O => CO ₂ + H ₂ (2)
At least a part of the inflowing fuel 8 is converted by the reforming process of the reformer 4 to generate hydrogen. The reforming reaction (1) takes place in the presence of a suitable steam reforming catalyst such as nickel. The reforming reaction (1) is extremely endothermic and has a heat of reaction of about 88,630 BTU / mole. The reforming reactions of other hydrocarbon fuels are endothermic as well. The reformed oil stream 44 includes carbon monoxide (CO), carbon dioxide (CO ₂ ), hydrogen (H ₂ ), unused fuel, and water. The reformed oil stream 44 is supplied to the separation unit 12, which separates hydrogen and carbon monoxide from the reformed oil stream 44 to produce a carbon dioxide rich stream 14, a hydrogen rich stream 16, and an exhaust gas stream 18. Is generated. In one embodiment, the exhaust gas stream 18 is recirculated back to the fuel inlet stream 8 and the mixed stream is supplied to the reformer 4 along with steam.

  The heat required for the endothermic reforming reaction (1) is supplied by the combustion heat from the combustor 6, and the combustor 6 is coupled to the reformer 4. Combustor 6 is configured to receive an incoming fuel stream 10 and a compressed oxidant stream 20. The incoming fuel stream 10 and the oxidant stream 20 can be premixed and injected into the combustor 6. In some embodiments, fuel and oxidant can be injected separately into the combustor 6. In some alternative embodiments, the fuel and oxidant are mixed partially or fully before being supplied to the combustor 6. The incoming fuel stream 10 can be any of, for example, hydrogen, natural gas, methane, naphtha, butane, propane, diesel, kerosene, aviation fuel, coal-derived fuel, biofuel, oxygenated hydrocarbon feedstock, and mixtures thereof. A suitable gas or liquid can be included. In some embodiments, the fuel can preferably include hydrogen or natural gas (NG) or a mixture thereof. In some other embodiments, a portion of the exhaust gas stream 18 from the separation unit 12 is used as fuel for the combustor 6. The compressed oxidant 20 from the compressor 24 can include any suitable oxygen-containing gas such as, for example, air, oxygen rich air, oxygen depleted air, and / or pure oxygen. In operation, the exemplary compressor 24 is a multi-stage compressor that includes a row of fixed vanes and rotating blades. The combustion process in the combustor 6 generates a hot gas stream 22.

  Returning to FIG. 1, the hot gas stream 22 from the combustor 6 is supplied to a gas turbine 26. The simultaneous production system 2 further includes a generator 28 attached to the gas turbine 26 and a heat recovery steam generator (hereinafter referred to as HRSG). The thermodynamic expansion of the hot gas stream 22 supplied to the gas turbine 26 generates the power that drives the gas turbine 26, so that the gas turbine generates electricity through the generator 28. Electricity generated from the generator 28 is converted into an appropriate form and supplied to a distribution power supply network (not shown). The expanded gas 30 from the gas turbine 26 is supplied to the HRSG 32 in order to recover the heat content of the expanded gas 30. A water stream 34 is supplied to the HRSG 32, which generates steam 38 by utilizing the recovered heat from the hot expanded gas 30 from the gas turbine 26. The cooled expanded gas 36 from the HRSG 32 is discharged into the atmosphere.

  Various exemplary embodiments of simultaneous production systems are shown in FIGS. As shown in FIGS. 2, 3, 4 and 5, all exemplary embodiments share the basic components of the illustrated simultaneous production system 2, in which the same elements have the same reference It is represented by a sign.

  A second exemplary embodiment of the simultaneous production system 50 is shown in FIG. According to the second embodiment, the separation unit 12 includes a heat exchanger 54, a shift reactor 56, and a separation device 62. In operation, the reformer 4 is in fluid communication with the heat exchanger 54. Water stream 52 is introduced into heat exchanger 54 where water is converted to steam 64 by utilizing the heat recovered from reformed oil stream 44 by reformer 4. The steam 64 generated in the heat exchanger 54 is used for the reforming process in the reformer 4.

The reformed oil stream 44 generated from the reformer 4 includes hydrogen (H ₂ ), carbon monoxide (CO), carbon dioxide (CO ₂ ), water, and unreacted fuel. The reformed oil stream 44 is cooled using a heat exchanger 54 to a temperature between about 200 degrees Celsius and about 400 degrees Celsius to produce a cooled reformed oil stream 58. Carbon monoxide and water in the cooled reformed oil stream 58 can react to produce more carbon dioxide. This can be achieved by an endothermic reaction (2) known as a water gas shift reaction. A CO ₂ lean cooled reformed oil stream 58 is fed to the shift reactor 56 to promote the water gas shift reaction in the presence of the catalyst. The outlet stream 60 from the shift reactor 56 contains unreacted fuel, carbon dioxide, water, hydrogen, and traces of unconverted carbon monoxide. The outlet stream 60 can also be referred to as a rich stream of hydrogen and carbon dioxide.

  The outlet stream 60 from the shift reactor 56, rich in hydrogen and carbon dioxide, is fed to a separator 62, which can further include a carbon dioxide separator. The carbon dioxide separator can separate carbon dioxide from the outlet stream 60 by applying various techniques known in the art including, but not limited to, pressure swing adsorption, chemisorption, and membrane separation.

  Pressure swing adsorption (PSA) can be used to separate carbon dioxide from a mixture of hydrogen-containing gases. With PSA technology at high partial pressure, solid molecular sieves can adsorb carbon dioxide more strongly than hydrogen. As a result, carbon dioxide is removed from this mixture as it passes through the adsorption bed under high pressure. Bed regeneration is achieved by depressurization and purging. Typically, for critical operations, multiple adsorption vessels are used for continuous separation of carbon dioxide, in which case another adsorption bed is used while one adsorption bed is being regenerated.

Another technique for separating carbon dioxide from a gas stream is chemisorption using oxides such as calcium oxide (Ca 2 O) and magnesium oxide (MgO) or combinations thereof. In one embodiment, under high temperature and pressure, CO ₂ is adsorbed by CaO to form calcium carbonate (CaCO ₃ ), thereby removing CO ₂ from the gas mixture. The adsorbent CaO is regenerated by calcination of CaCO _{3 which} can similarly modify CaCO ₃ to CaO.

Membrane separation techniques can also be used to separate carbon dioxide from a gas stream. Membrane processes are generally more energy efficient and easier to operate than adsorption processes. The membranes used for high temperature carbon dioxide separation include zeolite and ceramic membranes is selective to CO _2. However, the separation efficiency of membrane technology is low, and complete separation of carbon dioxide can be difficult to achieve by membrane separation. Normally, membrane separators function more efficiently at high pressures, and using a membrane separator to separate carbon dioxide from the outlet stream 60 from the shift reactor 56 is important for the outlet stream prior to CO ₂ separation. This can be achieved by further pressing 60.

Yet another technique used to separate CO ₂ from the outlet stream 60 can include, but is not limited to, chemisorption of CO ₂ with an amine. The outlet stream 60 can be cooled to a temperature suitable for using carbon dioxide chemisorption with amines. This technology is based on alkanolamine solvents that have the ability to adsorb carbon dioxide at relatively low temperatures and are more easily regenerated by increasing the temperature of the rich solvent. A carbon dioxide rich stream 14 is obtained after regeneration of the rich solvent. Solvents used in this technique can include triethanolamine, monoethanolamine, diethanolamine, diisopropanolamine, diglycolamine, methyldiethanolamine.

  In some embodiments, the carbon dioxide separator can include at least one adsorption bed in which PSA technology is used to separate carbon dioxide from the outlet stream 60. In some other embodiments, the carbon dioxide separator can include at least one adsorption vessel in which chemisorption techniques are used. In yet another embodiment, the carbon dioxide separator includes at least one membrane separator. Using various techniques described herein, the carbon dioxide rich stream 14 is generated from the separator 62. The carbon dioxide rich stream 14 can be exported for any other industrial application.

Separation device 62 can further include a hydrogen separator. Methods for separating hydrogen from other gases to produce a substantially pure hydrogen stream 16 include PSA and membrane separation. Various polymers can be used in hydrogen selective membranes that function at relatively low temperatures. In one embodiment, the hydrogen separation efficiency can be increased by combining a PSA unit and a CO ₂ separation membrane. In the first stage, H ₂ is separated by PSA technology. In the next stage, CO ₂ is separated by a CO ₂ selective membrane. Some polymer membranes exhibit good selective permeability in CO ₂ separation at relatively low temperatures.

In some embodiments, the hydrogen separator can use a cryogenic separation technique. Cryogenic separation can be used when multiple fractionation and multiple product recovery are important. In one embodiment, the outlet stream 60 from the shift reactor 56 is compressed to about 900 psia, is cooled to room temperature using the following condenser for liquefying CO _2. Hydrogen can be recovered from this process as a gas, while CO ₂ can be removed as a liquid from the bottom of the condenser. The hydrogen separator can further be integrated with a moisture separator.

  As shown in FIG. 2, three streams are recovered from the separator 62, namely a substantially pure hydrogen stream 16, a carbon dioxide rich stream 14 and an exhaust gas 18. The exhaust gas stream 18 from the separator 62 contains unreacted fuel, unseparated hydrogen, and water. In some embodiments, the exhaust gas stream 18 from the separator 62 further includes trace amounts of carbon dioxide and carbon monoxide. Stream 18 is recycled back to reformer 4 along with incoming fuel stream 8.

  In one embodiment, a portion of the hydrogen stream 16 is used as fuel for the combustion process in the combustor 6. In this exemplary embodiment shown in FIG. 2, complete carbon dioxide separation is achieved. Carbon dioxide is not formed during the combustion process of the combustor 6 when the fuel combusted in the combustor contains substantially pure hydrogen. Therefore, the hot gas 22 generated from the combustor does not contain carbon dioxide, and the gas 36 discharged into the atmosphere does not release carbon dioxide. The carbon dioxide produced in the reforming process is separated as a concentrated carbon dioxide stream 14 that is seized or sold in the commercial market depending on the demand for carbon dioxide. As shown in FIG. 2, a part of the steam 66 generated in the HRSG 32 is recycled to the reformer 4 to supply a sufficient amount of steam for the endothermic reforming reaction (1) and the exothermic water gas shift reaction (2). Cycled back. In some embodiments, another portion 38 of the steam generated by the HRSG 32 is sent to a steam turbine (not shown) for additional power generation.

FIG. 3 shows a third exemplary simultaneous production system in which the exhaust gas stream 18 from the separator 62 is recycled back to the combustor 6. As explained above, the exhaust gas stream 18 typically includes unburned _{fuel, H} 2, CO, and CO _2. Due to the separation of carbon dioxide as the concentrated carbon dioxide stream 14 in the separator 62, the carbon dioxide in the outlet stream 60 is substantially removed before the exhaust gas stream 18 is recycled to the combustor 6. As a result, the carbon dioxide generated in the combustor 6 and subsequently released into the atmosphere as the exhaust gas 36 contains a small amount of carbon dioxide as compared with the conventional combined cycle power generation system. Since carbon dioxide is removed in the pre-combustion stage before the exhaust gas 18 is recirculated to the combustor 6, carbon dioxide separation is partially achieved in the simultaneous production system as shown in FIG. If the outlet stream 60 from the shift reactor is fully enriched in carbon dioxide, carbon dioxide removal during the pre-combustion stage is more easily achieved. Since the hot compressed gas from the combustor contains nitrogen that dilutes the carbon dioxide concentration of the hot compressed gas stream 22 from the combustor 6, any post-combustion separation is difficult to achieve.

  FIG. 4 shows a fourth exemplary simultaneous production system in which the exhaust gas stream 18 is in fluid communication with the second combustion chamber 84. The exhaust gas stream 18 from the separator 62 is supplied to the second combustion chamber 84 along with an oxidant stream 82 such as air. In some embodiments, the oxidant stream 82 includes substantially pure oxygen, where the exhaust stream 86 from the second reformer does not include any diluent, such as nitrogen. The exhaust stream 86 is cooled by the HRSG 32, where the flow path of the exhaust stream 86 is separated from the flow path of the turbine exhaust 30 from the gas turbine 26. Since the fuel combusted in the combustor 6 contains substantially pure hydrogen, the advantage of the simultaneous production system shown in FIG. 4 is that carbon dioxide is separated. A portion 66 of the steam generated from the recovered heat from the exhaust gas 86 from the turbine exhaust 30 and the second combustion chamber 84 is recirculated to the reformer 4. The portion of steam 38 can be supplied to a steam turbine (not shown) for further power generation. In some embodiments, the cooled exhaust streams 36 and 85 from the HRSG 32 are exhausted to the atmosphere.

  FIG. 5 shows a fifth exemplary simultaneous production system in which the compressed air stream 20 is directed toward the recuperator 92, which is a known heat that includes a separate flow path. It is an exchange type. The compressed air stream 20 flows into the recuperator 92 through the first recuperator channel 96. The turbine exhaust 30 is mixed with the exhaust 86 from the second combustor 84 to form a mixed turbine exhaust stream 88. In some other embodiments, the exhaust 86 from the second combustor 84 and the exhaust 30 from the gas turbine 26 have separate flow paths in the recuperator 92, here to the combustor 84. The oxidant stream 82 contains substantially pure oxygen. As shown in FIG. 5, the mixed turbine exhaust stream 88 passes through the recuperator 92 in the second recuperator flow path 99 so that heat from the turbine exhaust 88 is transferred to the compressed air stream 20 and the turbine exhaust. The stream 88 is transmitted to the compressed air stream 20 without mixing. The heated compressed air stream 98 exits the recuperator 92 and flows to the combustor 6 where it supplies oxidant. Heating the compressed air stream 20 with the turbine exhaust 88 avoids the cost of a conventional heater or regenerative heat exchanger to raise the temperature of the oxidant, and the turbine exhaust stream 88 is discharged into the atmosphere. Cooled before being done. Subsequently, the cooled turbine exhaust stream 94 is supplied to the HRSG 32 where the incoming water stream 34 is heated to produce steam. The cooled turbine exhaust 36 is discharged into the atmosphere, and the generated steam 66 is recirculated back to the reformer 4.

In all exemplary embodiments in accordance with the techniques of the present invention shown in FIGS. 1, 2, 3, 4 and 5, the reformer 4 and the combustor 6 are combined. Cooling of the combustor 6 is achieved by endothermic reforming that reforms fuel and steam. The significant heat absorbed in the endothermic reforming process can cool the liner of the combustor 6 and further improve the combustor operability and flame stability. The simultaneous production system disclosed herein also achieves low flame temperatures by combusting hydrogen rich fuel in the combustor 6, as shown by the various embodiments described in the above section. , it is guaranteed to significantly reduce the formation of NO _x.

FIG. 6 shows a schematic diagram of an exemplary combustor-reformer with the reformer combined with the combustor. The combined reformer-combustor 100 is configured to be disposed within a cylindrical pressure shell 118. The thickness of the pressure shell is designed according to a proper criterion that depends on the maximum operating pressure of the reformer-combustor 100. The reforming process takes place in a tube 102 that is in intimate contact with the combustor 110, and the reformer 102 and the combustor 110 are concentric. The compressed air flows through the annular space 108 in the pressure shell, as shown by the air flow 106. Air enters the combustor 110 through the entry port 120. Fuel, such as hydrogen, natural gas or exhaust gas, is also sent to the combustor 110 at the same location (not shown). Air and fuel mixing is achieved in the mixing zone 122. Combustion zone 124 primarily generates combustion heat that dissipates radially and axially through surface 116 that contacts reformer 102. The standard temperature of the combustion zone 124 of the combustor 110 can be raised to about 1700 degrees Celsius, which is a temperature range sufficient to give much heat energy to the reforming process. In the heat transfer process from the combustor 110 to the reformer 102, the combustor liner is cooled, thereby increasing the life of the combustor. The fuel / steam mixture being reformed circulates in the annular space in the reforming tube 102 as indicated by the mixture channel 104. The reformate, which typically contains CO ₂ , CO, H ₂ , water, and unburned fuel, exits the reformer 102 through the opening 114.

  FIG. 7 shows the upper portion of yet another exemplary reformer combustor 130 with the combustor and reformer combined. The combustor 134 is a pressure vessel in which the cross section of the vessel decreases along the flow of combustion gas indicated by the flow path 140. This combustor has an annular structure as shown in FIG. 7 when rotated 360 degrees along the center line 154. The reformer 132 is another annular structure rotated 360 degrees along the same centerline 154. The combustor 134 includes an upper liner 148 that is in close contact with the reformer 132 and a bottom liner 160. The combustor 134 further includes a premixer 150 configured to have a port through which fuel and oxidant can pass into the combustor 134. In some embodiments, the premixed fuel and oxidant are injected into the combustor 134 through a nozzle that includes a swirler, the swirler including a plurality of swirl vanes that provide rotation to the incoming oxidant, and a rotation. A plurality of fuel spokes for distributing fuel to the oxidant stream. An oxidant 146 such as air is used to burn the combustor 134 and cool the bottom liner 160. The fuel and oxidant are mixed in an annular passage in the premix fuel nozzle prior to reaction in the combustor 134. The reformer 132 includes a passage 131 for introducing steam and a passage 158 for introducing reformed fuel. The reformed fuel and steam mixture flows through the passage 136 where the endothermic reaction (1) absorbs heat transferred from the combustor 134 to the reformer 132. Thermal energy is transferred from the combustor 134 to the reformer 132 by radial and axial heat dissipation by conduction and convection to cool the outer liner 148 of the combustor 134. The reformer 132 further includes a catalyst bed 156 containing a reforming catalyst such as nickel. The reformed oil flows out of the reformer 132 through the flow path 138. The inner liner 160 of the combustor 134 is cooled using a portion of the compressed air 146 where the air 142 circulates through the annular space 144 between the combustor inner liner 160 and the bottom shell 162.

  As described above, in various embodiments in accordance with the present technology, combustor cooling is achieved by endothermic reforming of fuels such as natural gas, and this cooling improves the overall efficiency of the system with simultaneous hydrogen and power. Production becomes possible. Significant heat absorption in the endothermic reforming process ensures that the combustor liner can be cooled and that flame stability is maintained or improved.

If a portion of the hydrogen produced in the co-production system is used as a combustor fuel, this can achieve a low flame temperature when the high hydrogen content fuel is combusted in the combustor. As such, a significant reduction in NO _x production is guaranteed. By separating carbon dioxide by pre-combustion in the separation unit, CO ₂ emissions to the atmosphere are reliably sequestered and limited. The disclosed simultaneous production method improves plant performance by transferring some of the waste heat from power generation to hydrogen production, thus improving plant efficiency and operability. The simultaneous production system disclosed herein has the flexibility to control the production of hydrogen by the reformed oil stream from the reformer and the generation of electrical energy according to demand. The hydrogen produced in the disclosed simultaneous production system can be utilized in several ways. The produced hydrogen can be recycled to the combustor and used as a fuel to achieve carbon dioxide-free emissions to the atmosphere. The produced hydrogen can be stored in a hydrogen storage unit that can contain a solid material such as a container, cylinder or metal hydride. The produced hydrogen can then be transported in gaseous form or liquid form such as using a liquefaction plant. The produced hydrogen can also be used as fuel in a fuel cell system composed of one or more fuel cells for additional power generation.

  Various embodiments of the present invention have been described in fulfilling various needs consistent with the present invention. It should be recognized that these embodiments are merely illustrative of the principles of various embodiments of the present invention. Reference numerals appearing in the claims do not narrow the scope of the invention but are intended to be more easily understood.

1 is a schematic process flow diagram of a first exemplary simultaneous production system. FIG. FIG. 3 is a schematic process flow diagram of a second exemplary simultaneous production system. FIG. 4 is a schematic process flow diagram of a third exemplary simultaneous production system. FIG. 10 is a schematic process flow diagram of a fourth exemplary simultaneous production system. FIG. 10 is a schematic process flow diagram of a fifth exemplary simultaneous production system. 1 is a schematic diagram of an exemplary combustor reformer. FIG. FIG. 4 is a cross-sectional view of another exemplary combustor reformer.

Explanation of symbols

4 reformer 6 combustor 8 reformer fuel 10 fuel 12 separation unit 18 exhaust gas 22 high-temperature compressed gas 26 gas turbine 30 expanded gas 32 heat recovery steam generator, HRSG
44 reformed oil 54 heat exchanger 56 water gas shift reactor 60 hydrogen and carbon dioxide rich stream

Claims (10)

A system for simultaneous production of hydrogen and electrical energy,
A reformer (4) configured to receive the reformer fuel (8) and steam to produce a hydrogen-rich reformate (44);
A separation unit (in fluid communication with the reformer (4)) configured to receive the reformed oil (44) and separate hydrogen from the reformed oil (44) to produce exhaust gas (18). 12)
A combustor (6) configured to receive fuel (10) for combustion to produce thermal energy and hot compressed gas (22), coupled to the reformer (4);
A gas turbine (26) for expanding the hot compressed gas (22) to produce electrical energy and expanded gas (30);
With
A system characterized in that at least part of the thermal energy from the combustor (6) is used to produce the reformed oil (44) in the reformer (4).   The system of claim 1, wherein at least a portion of the exhaust gas (18) is recycled back to the reformer (4) after separating hydrogen.   The system of claim 1, wherein the reformate (44) further comprises carbon monoxide, carbon dioxide, and the reformer fuel.   The system of claim 3, wherein the separation unit (12) further comprises a water gas shift reactor (56) that converts carbon monoxide to carbon dioxide and converts it to hydrogen and a carbon dioxide rich stream (60).   The system of claim 1, further comprising a heat exchanger (54) for generating steam.   The system according to claim 1, wherein the hydrogen produced from the separation unit (12) is used as fuel for the combustor (6).   The system of claim 1, further comprising a heat recovery steam generator (HRSG) (32) for generating steam and a steam turbine. A system for simultaneous production of hydrogen and electrical energy,
A reformer (4) configured to receive reformer fuel and steam to produce hydrogen-rich reformate (44);
A combustor (6) configured to receive fuel (10) for combustion to produce thermal energy and hot compressed gas (22), coupled to the reformer (4);
A separation unit (in fluid communication with the reformer (4)) configured to receive the reformed oil (44) and separate hydrogen from the reformed oil (44) to produce exhaust gas (18). 12)
With
At least a portion of the thermal energy from the combustor (6) is used to produce the reformed oil (44) in the reformer (4);
A gas turbine (26) for expanding the hot compressed gas (22) to generate electrical energy and an expanded gas (30);
At least a portion of the thermal energy from the combustor (6) is used to produce the reformed oil (44) in the reformer (4), and the separation unit (12) is used for the reforming. A system configured to separate carbon dioxide from oil (44) and recirculate at least a portion of the exhaust gas (18) to the reformer (4). A method for the simultaneous production of hydrogen and electrical energy comprising:
Reforming the reformer fuel and steam mixture in the reformer (4) to produce a hydrogen rich reformate (44);
Separating hydrogen from the reformed oil (44) to produce exhaust gas (18);
Combusting fuel in a combustor (6) coupled to the reformer (4) to produce thermal energy and hot compressed gas (22);
Expanding the hot compressed gas (22) in an expanding gas turbine (26) to produce electrical energy and expanded gas (30);
Including
A method in which at least a portion of the thermal energy from the combustor (6) is used to produce the reformed oil (44) in the reformer (4). A combustor reformer system comprising:
A combustor (6) configured to receive and burn fuel and oxidant to produce hot compressed gas (22) and thermal energy;
A reformer (4) configured to be in intimate contact with the combustor (6) and to receive reformer fuel and steam to produce hydrogen-rich reformate (44);
With
The reformer (4) is coupled to the combustor (6), and at least a portion of the thermal energy from the combustor (6) is transferred to the reformed oil (44) in the reformer (4). A combustor reformer system characterized in that it is used to produce

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